CA2492720C - A process for decreasing the amount of cholesterol in a marine oil using a volatile working fluid - Google Patents

A process for decreasing the amount of cholesterol in a marine oil using a volatile working fluid Download PDF

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Publication number
CA2492720C
CA2492720C CA2492720A CA2492720A CA2492720C CA 2492720 C CA2492720 C CA 2492720C CA 2492720 A CA2492720 A CA 2492720A CA 2492720 A CA2492720 A CA 2492720A CA 2492720 C CA2492720 C CA 2492720C
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Prior art keywords
cholesterol
marine oil
process according
working fluid
lowered
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CA2492720A1 (en
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Sverre Sondbo
Olav Thorstad
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Pronova Biopharma Norge AS
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Pronova Biopharma Norge AS
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Priority claimed from SE0202188A external-priority patent/SE0202188D0/en
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    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K50/00—Feeding-stuffs specially adapted for particular animals
    • A23K50/80—Feeding-stuffs specially adapted for particular animals for aquatic animals, e.g. fish, crustaceans or molluscs
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
    • A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
    • A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
    • A23D9/02—Other edible oils or fats, e.g. shortenings, cooking oils characterised by the production or working-up
    • A23D9/04—Working-up
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K20/00—Accessory food factors for animal feeding-stuffs
    • A23K20/10—Organic substances
    • A23K20/158—Fatty acids; Fats; Products containing oils or fats
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
    • A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
    • A23L33/115—Fatty acids or derivatives thereof; Fats or oils
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P13/00—Drugs for disorders of the urinary system
    • A61P13/12—Drugs for disorders of the urinary system of the kidneys
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P25/00—Drugs for disorders of the nervous system
    • A61P25/28—Drugs for disorders of the nervous system for treating neurodegenerative disorders of the central nervous system, e.g. nootropic agents, cognition enhancers, drugs for treating Alzheimer's disease or other forms of dementia
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P29/00—Non-central analgesic, antipyretic or antiinflammatory agents, e.g. antirheumatic agents; Non-steroidal antiinflammatory drugs [NSAID]
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P3/00—Drugs for disorders of the metabolism
    • A61P3/02—Nutrients, e.g. vitamins, minerals
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P3/00—Drugs for disorders of the metabolism
    • A61P3/06—Antihyperlipidemics
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P43/00—Drugs for specific purposes, not provided for in groups A61P1/00-A61P41/00
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P9/00—Drugs for disorders of the cardiovascular system
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P9/00—Drugs for disorders of the cardiovascular system
    • A61P9/10—Drugs for disorders of the cardiovascular system for treating ischaemic or atherosclerotic diseases, e.g. antianginal drugs, coronary vasodilators, drugs for myocardial infarction, retinopathy, cerebrovascula insufficiency, renal arteriosclerosis
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P9/00—Drugs for disorders of the cardiovascular system
    • A61P9/12—Antihypertensives
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/006—Refining fats or fatty oils by extraction
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/12—Refining fats or fatty oils by distillation
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/12—Refining fats or fatty oils by distillation
    • C11B3/14—Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
    • C11C3/10—Ester interchange
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F16—ENGINEERING ELEMENTS AND UNITS; GENERAL MEASURES FOR PRODUCING AND MAINTAINING EFFECTIVE FUNCTIONING OF MACHINES OR INSTALLATIONS; THERMAL INSULATION IN GENERAL
    • F16D—COUPLINGS FOR TRANSMITTING ROTATION; CLUTCHES; BRAKES
    • F16D55/00—Brakes with substantially-radial braking surfaces pressed together in axial direction, e.g. disc brakes
    • F16D55/24—Brakes with substantially-radial braking surfaces pressed together in axial direction, e.g. disc brakes with a plurality of axially-movable discs, lamellae, or pads, pressed from one side towards an axially-located member
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2200/00—Function of food ingredients
    • A23V2200/30—Foods, ingredients or supplements having a functional effect on health
    • A23V2200/3262—Foods, ingredients or supplements having a functional effect on health having an effect on blood cholesterol
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F16—ENGINEERING ELEMENTS AND UNITS; GENERAL MEASURES FOR PRODUCING AND MAINTAINING EFFECTIVE FUNCTIONING OF MACHINES OR INSTALLATIONS; THERMAL INSULATION IN GENERAL
    • F16D—COUPLINGS FOR TRANSMITTING ROTATION; CLUTCHES; BRAKES
    • F16D55/00—Brakes with substantially-radial braking surfaces pressed together in axial direction, e.g. disc brakes
    • F16D2055/0004—Parts or details of disc brakes
    • F16D2055/0008—Brake supports
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
    • Y02A40/80—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in fisheries management
    • Y02A40/81—Aquaculture, e.g. of fish
    • Y02A40/818—Alternative feeds for fish, e.g. in aquacultures

Abstract

The invention relates to a process for decreasing the amount of cholesterol in a mixture comprising a marine oil, the marine oil containing the cholesterol, which process comprises the steps of adding a volatile working fluid to the mixture, where the volatile working fluid comprises at least one of a fatty acid ester, a fatty acid amide and a hydrocarbon, and subjecting the mixture with the added volatile working fluid to at least one stripping processing step, in which an amount of cholesterol present in the marine oil in free form is separated from the mixture together with the volatile working fluid. The present invention also relates to a volatile cholesterol decreasing working fluid and a health supplement and a pharmaceutical, based on a marine oil, prepared according to the process mentioned above.

Description

Pronova Biocare AS

A PROCESS FOR DECREASING THE AMOUNT OF CHOLESTEROL
IN A MARINE OIL USING A VOLATILE WORKING FLUID
FIELD OF THE INVENTION
This invention relates to a process for decreasing the amount of cholesterol in a mixture comprising a ma-rine oil, containing the cholesterol. The present inven-tion also relates to a volatile cholesterol decreasing working fluid, a health supplement and a pharmaceutical, prepared according to the process mentioned above.
BACKGROUND OF THE INVENTION
It is known that cholesterol is an important steroid found in the lipids (fats) in the bloodstream and in all body's cells in mammals. Cholesterol is used to form cell membranes, some hormones and other needed tissues. A mam-mal will get cholesterol in two ways; the body produces some of it, and the rest comes from products that the mammal consumes, such as meats, poultry, fish, eggs, but-ter, cheese and whole milk. Food from plants like fruits, vegetables and cereals do not include cholesterol.
Cholesterol and other fats can't dissolve in the blood. They have to be transported to and from the cells by special carriers called lipoproteins, named on basis of their density. Low-density lipoprotein, or LDL, trans-port cholesterol from the liver to peripheral tissues and LDL transported cholesterol is known as the "bad" choles-terol, because too much LDL cholesterol can clog the ar-teries to the heart and increase the risk of heart at-tack. High-density lipoprotein, or HDL, transport choles-CONFIRMATION COPY
2 terol back to the liver where surplus cholesterol is dis-posed of by the liver as bile acids. HDL transported cho-lesterol is known as the "good" cholesterol and high lev-els of HDL may reduce cholesterol deposits in arteries.
For an organism to remain healthy, there has to be an in-tricate balance between the biosynthesis of cholesterol and its utilization, so that arterial deposition is kept at a minimum.
In e.g. marine oils, cholesterol is stored as "free"
respectively as "bound" cholesterol. In the bound form, cholesterol is esterified on the OH-group by a fatty acid.
HO
Structural formula of cholesterol The commercially important polyunsaturated fatty ac-ids in marine oils, such as fish oil, are preferably EPA
(eicosapentaenoic acid, C20:5), DHA (docosahexaenoic acid, C22:6). The full nomenclature of these acids ac-cording to the IUPAC system is: EPA cis-5,8,11,14,17-eicosapentaenoic acid, DHA cis-4,7,10,13,16,19-docosahexaenoic acid. For many purposes it is necessary that the marine oils should be refined in order to in-
3 crease the content of EPA and/or DHA to suitable levels, or to reduce the concentrations of, or even eliminate, certain other substances which occur naturally in the raw oil, e.g. cholesterol.
The fatty acids EPA and DHA are also proving in-creasingly valuable in the pharmaceutical and food sup-plement industries in particular. It is also very impor-tant for fish oils and other temperature sensitive oils (i.e. oils that contains long chain polyunsaturated fatty acids) to keep the load of the temperature as low as pos-sible. Concerning the amount of cholesterol in the oils, it is specially a problem in fish oils and milk fat.
Further, as the link between high serum cholesterol levels and heart disease has become increasingly appar-ent, cholesterol-free and cholesterol-reduced food prod-ucts have become more attractive to consumers, and food products that have no or reduced cholesterol are gaining popularity as well as an increasing share of the market.
Consequently, removal or reduction of cholesterol in high cholesterol foods has the potential to substantially in-crease marketability and value.
The removal or reduction of cholesterol in marine oils is not a trivial matter. Several different tech-niques to accomplish this task have been developed, each with varying levels of success. The content of choles-terol in marine oils will become a much more important parameter for the process industry in the future.
Some methods of treating a fish oil is known from the prior art. Such methods include conventional vacuum steam distillation of fish oils at high temperatures which creates undesirable side reactions, decreases the content of EPA and DHA in the oil and the resulting prod-
4 uct has a poor flavour stability and poor resistance to oxidation.
SUMMARY OF THE INVENTION
One object of the invention is to offer an effective process for decreasing the amount of cholesterol in a mixture comprising a marine oil, containing the choles-terol, preferably by decreasing and separating the amount of cholesterol present in free form.
According to a first aspect of the invention, this and other objects are achieved with a process for de-creasing the amount of cholesterol in a mixture compris-ing a marine oil, the marine oil containing the choles-terol, which process comprises the steps of adding a volatile working fluid to the mixture, where the volatile working fluid comprises at least one of a fatty acid ester, a fatty acid amide and a hydrocarbon, and subjecting the mixture with the added volatile work-ing fluid to at least one stripping processing step, in which an amount of cholesterol in the marine oil is sepa-rated from the mixture together with the volatile working fluid. Most preferably, the amount of cholesterol present in the marine oil that is separated from the mixture to-gether with the volatile working fluid is constituted by cholesterol in free form. Herein, "an amount" is inter-preted to include decreasing of an amount up to almost 100% of cholesterol present in free form, i.e. a substan-tial removal of cholesterol in free form from a marine fat or oil composition, at low mixture flow rates. The content of bound cholesterol is less affected by the stripping process according to the invention, since cho-lesterol in bound form has a higher boiling point com-pared to the working fluid according to the invention.
5 PCT/IB2003/002776 The use of a volatile working fluid, where the vola-tile working fluid comprises at least one of a fatty acid ester, a fatty acid amide and a hydrocarbon, or any com-bination thereof, in a stripping process (or processing 5 step) for decreasing the amount of cholesterol present in a marine oil in free form has a number of advantages.
An advantage of using a volatile working fluid in a stripping process is that the cholesterol present in free form can more easily be stripped off together with the volatile working fluid. Preferably, this is possible as long as the volatile working fluid is essentially equally or less volatile than the cholesterol that shall be re-moved from the oil mixture. The stripped cholesterol pre-sent in free form and the volatile working fluid will be found in the distillate. When the volatile working fluid have the mentioned property, in combination with benefi-cial stripping process conditions, it is possible to separate, or strip off, almost all cholesterol present in a marine oil in free form more effectively. The effect of adding a volatile working fluid to a marine oil mixture before stripping is larger and also more commercial use-ful, compared to a general process for decreasing choles-terol in an oil mixture, at higher flow rates. Herein, "high flow rates" is interpreted to include mixture flow rate in the interval of 80-150 kg/h~mz. Under the process conditions mentioned above, the use of a volatile working fluid open up for a much better utilization of the capac-ity of the process equipment and a more rapid stripping process.
Further, according to the present stripping process it is also possible to decrease an effective amount of cholesterol present in a marine oil in free form at lower temperatures, preferably at a temperature in the interval
6 of 150 - 220°C, compared to the techniques known from the prior art. It is especially important to keep the tem-perature as low as possible during processing of marine oils, such as fish oils, and other temperature accommo-dating oils (i.e. oils comprising long chains of polyun-saturated fatty acids). This is not so critical for oils not included above. In addition, the volatile working fluid according to the invention allows cholesterol pre-sent in free form to be stripped off by e.g. molecular distillation even from oils of lower quality, i.e. oil for feed purposes.
In a preferred embodiment of the present invention the volatile working fluid is an organic solvent or sol-vent mixture with a volatility comparable to the choles-terol in free form. The volatile working fluid of the present invention is at least one of a fatty acid ester, a fatty acid amide, and a hydrocarbon, also including any combinations thereof.
In another preferred embodiment the volatile working fluid comprises at least one fatty acid ester composed of C10-C22 fatty acids and C1-C4 alcohols, or a combination of two or more fatty acid ester each composed of C10-C22 fatty acids and C1-C4 alcohols. Preferably, the volatile working fluid is at least one of amides composed of C10-C22 fatty acids and C1-C4 amines, C10-C22 free fatty acids, and hydrocarbons with a total number of carbon atoms from 10 to 40. Most preferably, the volatile working fluid is a mixture of fatty acids from marine oils, e.g. fish body oil and/or fish liver oil, and/or ethyl or methyl esters of such marine fatty acids.
In another embodiment of the invention a volatile working fluid may be produced by subjecting fats or oils from an available source, for instance fats or oils
7 obtained from at least one of animal, microbial or vegetable origin, to an inter-esterification process, in which process the triglycerides in the fats or oils are converted into esters of aliphatic alcohols.
Additionally, a bio-diesel and/or a mineral oil can be used as a volatile working fluid. In the case when the volatile working fluid is a biodiesel, it can be produced by a process, which is in common use for production of engine fuels (biodiesel), and therefore also known by a man skilled in the art, which process comprises mixing the fat or oil with a suitable amount of aliphatic alcohol, adding a suitable catalyst and heating the mixture for a period of time. Similar esters of aliphatic alcohols may also be produced by a high-temperature catalytic direct esterification process reacting a free fatty acid mixture with the appropriate aliphatic alcohol. The fatty acid ester mixture produced in this manner may be used as a volatile working fluid as it is, but normally the conversion to esters of aliphatic alcohols is not complete, the conversion process preferably leaving some un-reacted non-volatile glycerides in the mixture. Further, some fats or oils may also contain certain amounts of non-volatile, non-glyceride components (e. g. polymers). Such non-volatile components will be transferred to, and mixed with the final product, which product is low in cholesterol, when the fatty acid ester mixture is used as working fluid. A
working fluid produced in this manner should therefore be subjected to a distillation, preferably a molecular and/or short path distillation, in at least one step, which distillation process generates a distillate more suitable to be used as a new volatile working fluid.
8 In addition, the volatile working fluid according to the invention allows cholesterol to be stripped off by e.g. molecular distillation even from oils of lower qual-ity.
In another preferred embodiment of the process, at least one of a fatty acid ester and a fatty acid amide constituting said volatile working fluid is obtained from at least one of a vegetable, microbial and animal fat or oil, being edible or for use in cosmetics. Preferably, the animal fat or oil is a marine oil, e.g. a fish oil or an oil from other marine organism e.g. sea mammals. It is also possible that the fatty acid esters mentioned above can e.g. be a byproduct from distillation of an ethyl es-ter mixture prepared by ethylation of preferably a fish oil. In the process industry trade with intermediates is increasing and opens up for an extra financial income.
In fish oils cholesterol is typically present in concentrations of 5-10 mg/g, but higher concentrations have been observed. In this case 2-4 mg/g is typically bound cholesterol and 3-6 mg/g is free cholesterol. Free cholesterol can be effectively removed by adding a volatile working fluid prior to at least one of the stripping processes according to the invention.
In another embodiment of the process according to the invention, the marine oil containing saturated and unsaturated fatty acids in the form of triglycerides, and the marine oil is obtained from fish and/or sea mammals.
Marine oils that contains no or reduced amounts of cholesterol present in free form are gaining popularity as well as an increasing share of the market.
It is important to note that the invention is not limited to procedures were the working fluid is prepared from the same origin as the oil that is being purified.
9 In a preferred embodiment of the invention, the ratio of (volatile working fluid):(marine oil) is about 1:100 to 15:100. In a more preferred embodiment the ratio of (volatile working fluid):(marine oil) is about 3:100 to 8:100.
In a preferred embodiment of the invention, said stripping process step is carried out at temperatures in the interval of 120-270 °C.
In a most preferred embodiment, the stripping processing step is carried out at temperatures in the interval of 150-220 °C. By adding a volatile working fluid to the marine oil mixture at this temperatures the invention surprisingly shows that even termolabile polyunsaturated oils can be treated with good effect, without causing degradation of the quality of the oil.
In another preferred embodiment, the stripping processing step is carried out at a pressure below 1 mbar.
In further preferred embodiment, the stripping processing step is at least one of a thin-film evaporation process, a molecular distillation or a short-path distillation, or any combination thereof. If at least one stripping process step is a thin-film evaporation the process is also carried out at mixture flow rates in the intervall of 30-150 kg/h'm2, most preferably in the range of 80-150 kg/h'mz. The effect of adding a volatile working fluid to a marine oil mixture before stripping is larger and also more commercial useful, compared to a general process for decreasing cholesterol present in a marine fat or oil in free form at higher flow rates.
By using a stripping process, e.g. a distillation method, for decreasing the amount of cholesterol present in a marine oil in free form, the marine oil mixture comprising a volatile working fluid, it is possible to carry out the stripping processes at lower temperatures, which spare the oil and is at the same time favourable to 5 the end oil product.
Another embodiment of the present invention is a stripping process wherein a working fluid is added to a mixture comprising a marine oil, containing cholesterol, prior to a thin-film evaporation process, and the vola-
10 tile working fluid comprises at least one of a fatty acid ethyl ester and a fatty acid methyl ester (or any combi-nations thereof), and subjecting the mixture with the added working fluid to a thin-film evaporation step, in with an amount of cholesterol present in free form in the marine oil is separated from the mixture together with the volatile working fluid.
In a preferred embodiment according to the invention the stripping process is carried out by a molecular distillation in the following intervals; mixture flow rates in the interval of 30-150 kg/h~m2, temperatures in the interval of 120-270 °C and a pressure below 1 mbar.
In a most preferred embodiment of the invention the molecular distillation is carried out at temperatures in the interval of 150-220°C and at a pressure below 0,05 mbar, or by a thin-film process, which process is carried out at 80-150 kg/h'm2 or at flow rates in the range of 800-1600 kg/h at a heated thin film area of 11 m2; 73-146 kg/h'm2. Please note, that the present invention can also be carried out in one or more subsequent stripping processing steps.
In another preferred embodiment of the present invention, a volatile cholesterol decreasing working fluid, for use in decreasing an amount of cholesterol
11 present in a marine oil in free form, the volatile working fluid is comprising at least one of a fatty acid ester, a fatty acid amide and a hydrocarbon, with essentially equally or less volatility compared to the cholesterol that is to be separated from the marine oil, or any combination thereof.
Preferably, the volatile cholesterol decreasing working fluid is generated as a fractionation product.
Additionally, the volatile cholesterol decreasing working fluid is a by-product, such as a distillation fraction, from a regular process for production of ethyl and/or methyl ester concentrates. This by-product according to the invention can be used in a new process preferably for fat or oil being edible or for use in cosmetics. More preferably, the volatile cholesterol decreasing working fluid, for use in decreasing an amount of cholesterol present in a marine fat or oil, can be a by-product (a distillate fraction) from a regular process for production of ethyl ester concentrates, wherein a mixture comprising an edible or a non-edible fat or oil, preferably a fish oil, is subjected to an ethylating process and preferably a two-step molecular distillation.
In the two-step molecular distillation process a mixture consisting of many fatty acids on ethyl ester form is separated from each other in; a volatile (light fraction), a heavy (residuum fraction) and a product fraction. The volatile fraction from the first distillation is distilled once more and the volatile fraction from the second distillation process is then at least composed of the volatile working fluid, preferably a fatty acid ethyl ester fraction. This fraction consists of at least one of C14 and C16 fatty acids and at least one of the C18 fatty acids from the fat or oil, and is
12 therefore also compatible with the edible or non-edible oil. The fraction can be redistilled one or more times if that is deemed to be suitable. This prepared working fluid can then be used as a working fluid in a new process for decreasing the amount of cholesterol present in a marine oil in free form, wherein the edible or non-edible fats or oils and the marine oil are of the same or different types.
In another preferred embodiment of the invention the volatile working fluid comprises at least one of an ester and/or an amide composed of shorter fatty acids and longer alcohols or amines, or any combination thereof.
In a preferred embodiment of the invention, the volatile cholesterol decreasing working fluid, for use in decreasing an amount of cholesterol present in a marine oil, is preferably a fatty acid ester (e. g. fatty acid ethyl ester or fatty acid methyl ester) or a fatty acid amide obtained from at least one of vegetable, microbial and animal fat or oil, or any combination thereof.
Preferably, said animal fat or oil is a marine oil, for instance a fish oil and/or an oil from sea mammals.
In another embodiment of the invention, a volatile cholesterol decreasing working fluid according to the present invention, is used in a process for decreasing the amount of cholesterol in a mixture comprising a ma-rine oil, the marine oil containing the cholesterol, in which process the volatile working fluid is added to the mixture and then the mixture is subjected to at least one stripping processing step, preferably a thin-film evapo-ration process, a molecular distillation or a short-path distillation or any combination thereof, and in which process an amount of cholesterol present in the marine oil in free form is separated from the oil mixture
13 In a more preferred embodiment, the volatile choles-terol decreasing working fluid is a by-product, such as a distillate fraction, from a regular process for produc-tion of ethyl and/or methyl ester concentrates.
In another preferred embodiment a health supplement, or a pharmaceutical containing oil (end) products with a decreased amount of cholesterol, preferably strongly lim-ited amounts of cholesterol present in free form, pre-pared according to at least one of the previously men-tinned processes is disclosed. For the pharmaceutical and food supplement industries, marine oils often is processed in order to increase the content of EPA and/or DHA to suitable levels and the removal or reduction of cholesterol have the potential to substantially increase marketability and value. Therefore, the present invention also discloses a health supplement and a pharmaceutical respectively, containing at least a marine oil, such as fish oil, which marine oil is prepared according to the previously mentioned process, in order to decrease the total amount of cholesterol present in the marine oil. It shall be noted that the invented process may also be used for marine oils which has not been processed in order to increase the content of EPA and/or DHA to suitable levels.
In another embodiment of the invention the pharmaceutical and/or health supplement is preferably intended for treating cardiovascular diseases (CVD) and inflammatory diseases, but they also have positive effects on other CVD risk factors such as the plasma lipid profile, hypertension and vascular inflammation. In more preferred embodiment of the invention the pharmaceutical and/or health supplement comprises at least one of EPA/DHA triglycerides/ethyl esters and is
14 intended for a range of potential therapeutic applications including; treatment of hypertriglyceridaemia, secondary prevention of myocardial infarction, prevention of atherosclerosis, treatment of hypertension, mental disorders and/or kidney disease and to improve children's learning ability.
Preferably, the pharmaceutical and/or health supple-ment prepared according to at least one of the previously mentioned processes is based on fish oil.
Further, the present invention also disclose a marine oil product, prepared according to at least one of the previously mentioned processes. Preferably, the marine oil product is based on fish oil or a fish oil composition.
In another preferred embodiment the stripping proc-ess is followed by a trans-esterification process. Pref-erably, the stripping processing step is followed by the steps of; subjecting the stripped marine oil mixture to at least one trans-esterification reaction with a C1-C6 alcohol under substantially anhydrous conditions, and in the presence of a suitable catalyst (a chemical catalyst or an enzyme) to convert the fatty acids present as triglycerides in the marine oil mixture into esters of the corresponding alcohol, and thereafter subjecting the product obtained in the step above to at least one or more distillations, preferably one or more molecular dis-tillations.
After the traps-esterification reaction some glyc-Brides and most of the bound cholesterol will remain un-reacted. Both the unreacted glycerides and the bound (es-terified) cholesterol will have higher boiling points than the valuable esters of polyunsaturated fatty acids, and will therefore be concentrated in the residue (waste) fraction. Thereby a substantial reduction in bound cho-lesterol can be obtained in the distillate (product) fraction..
By combining the steps of first stripping the cho-5 lesterol in free form from the marine oil triglycerides using a volatile working fluid, followed by catalysed es-terification of the marine oil with a C1-C6 alcohol under substantially anhydrous conditions, and thereafter dis-tillation under conditions suitable to enrich the bound 10 cholesterol in the residium (waste) fraction, a fatty acid ester product with a significant reduction in both free and bound cholesterol can be produced. More prefera-bly, said C1-C6 alcohol is ethanol.
In another preferred embodiment of the invention the
15 volatile working fluid comprises at least one of an es-ter, amides and/or esters composed of longer fatty acids and shorter alcohols or amines, or any combination thereof .
BRIEF DESCRIPTION OF THE DRAWINGS
The advantages and details of the present invention will become apparent from the following description when taken in conjugation with the accompanying drawings, in which;
FIG 1 is a schematic flow chart of one embodiment illustrating a method for decreasing the amount of cho-lesterol in a marine oil, by adding a volatile working fluid prior to a molecular distillation.
DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
A number of preferred embodiments of the process for decreasing the amount of cholesterol in a mixture com-
16 prising a volatile working fluid and a marine oil, con-taming the cholesterol, will be disclosed below.
A first embodiment of a process for decreasing the amount of cholesterol in a marine oil by adding a vola-tile working fluid prior to a molecular distillation is presented in figure 1. The starting marine oil in the first embodiment of the invention is a fish oil whether freshly refined, reverted or mixtures thereof character-ized by an initial or native cholesterol level. The exact amount of cholesterol varies depending upon such factors as fish species, seasonality, geographical catch location and the like.
As used herein the term molecular distillation is a distillation process performed at high vacuum and pref-erably low temperature (above 120°C). Herein, the conden-sation and evaporation surfaces are within a short dis-tance from each other, so as to cause the least damage to the oil composition.
The molecular distillation plant (1) illustrated in figure 1, comprises a mixer (2), a pre-heater (3), a de-gasser (4), a distillation unit (5) and a vacuum pump (6). In accordance with this embodiment, a volatile work-ing fluid comprising an ethyl ester fraction (6°s relative to the oil) is added to a fish oil mixture and blended in a mixer (2). The fish oil mixture is then optionally passed through a means for controlling the oil feed rate, such as an ordinary throttling valve. The fish oil mix-ture is then preheated with a heating means (3) such as a plate heat exchanger to provide a preheated fish oil mix-ture. The mixture is then passed through a degassing step (4) and admitted into the short path evaporator (5), a tube (7) including the condensation (8) and evaporation (9) surface. The fish oil mixture to be concentrated is
17 picked up as it enters the tube (7a) by rotating blades (not shown). The blades extend nearly to the bottom of the tube and mounted so that there is a clearance of about 1,3 mm between their tips and the inner surface of the tube. In addition, the blades are driven by an exter-nal motor. The fish oil mixture is thrown against the tube wall and is immediately spread into a thin film and is forced quickly down (A) the evaporation surface. The film flows down by gravity, and as it falls the light and heavy fractions are separated because of differences in boiling point.
Heated walls and high vacuum strips off the volatile working fluid together with the cholesterol, i.e. the more volatile components (distillate) is derived to the closely positioned internal condenser (8), the less vola-tile components (residue) continues down the cylinder.
The resulting fraction, the stripped fish oil mixture containing at least the fatty acids EPA and DHA is sepa-rated and exit through an individual discharge outlet (10) .
In a second embodiment a falling film evaporator is used. In falling film evaporators liquid and vapours flow downwards in parallel flow. The liquid to be concen-trated, herein the fish oil mixture, is preheated to boiling temperature. The oil mixture enters the heating tubes via a distribution device in the head of the evapo-rator, flows downward at boiling temperature, and is par-tially evaporated. This gravity-induced downward movement is increasingly augmented by the co-current vapour flow.
Falling film evaporators can be operated with low tem-perature differences between the heating media and the boiling liquid, and they also have short product contact times, typically just a few seconds per pass.
18 In a third embodiment of the invention the process is carried out by a short path distillation, which in-cludes the use of a short path evaporator that integrates the features and advantages of thin film or wiped film evaporators but adds internal condensing for applica-tions. Short path evaporators are widely used in fine and specialty chemicals for thermal separation of intermedi-ates, concentration of high value products, and molecular distillation under fine vacuum conditions. Their key fea-tures make them uniquely suitable for gentle evaporation and concentration of heat sensitive products at low pres-sures and temperatures.
In a fourth embodiment of the invention the strip-ping process is followed by the steps of subjecting the stripped marine oil mixture to at least one trans-esterification reaction with a C1-C6 alcohol under sub-stantially anhydrous conditions and thereafter subjecting the product obtained in the step above to at least one or more distillations, preferably one or more molecular dis-tillations. The key step in all trans-esterification re-actions is the reaction between an ester mixture, com-posed of fatty acids bound to an alcohol A, and an alco hol B where the reaction products are an ester mixture, composed of the same fatty acids bound to alcolhol B, and alcohol A as shown in this general formula:
kat R-CO 0 R~ + Hp-R2 ~ R-C0-0 R2 + R~-OH
The reaction is preferably catalysed and the reac-tion is an equilibrium and the yield of the expected fatty acid ester is to a large extent controlled by the concentration of the alcohols. Herein, for instance the
19 stripping process is followed by a catalysed trans-esterification of marine oil triglycerides. The separa-tion of the ethyl ester fraction from the fraction con-taming the unreacted glycerides and bound cholesterol is suitably carried out by at least one of a molecular dis-tillation technique, whereby the less volatile residual mixture can be readily removed from the relatively vola-tile ethyl esters.
It should be understood that many modifications of the above embodiments of the invention are possible within the scope of the invention such as the latter is defined in the appended claims. It will be apparent for one skilled in the art that various changes and modifica-dons, i.e. other combinations of temperatures, pres-sures, and flow rates during the stripping process can be made therein without departing from the spirit and scope thereof.
EXAMPLES
The invention will now be illustrated by means of the following non-limiting example. This example is set forth merely for illustrative purposes and many other variations of the process may be used. The example below summarize some results from different purification of fish oils by molecular distillation.
~'YZ1MDT.~' 'I
A stripping process for decreasing the amount of choles-terol present in a fish oil mixture in free form with re-spectively without using a volatile working fluid This example shows an industrial scale process for decreasing the amount of cholesterol in a refined fish oil mixture in free form, with and without adding a vola-tile working fluid to the fish oil mixture, and subject-ing the mixture to a molecular distillation process.
Herein, an Anchovy oil from Peru, with a fatty acid 5 composition of 18% EPA and 12°s DHA was used. The oil con-tains about 9 mg cholesterol/g fish oil, of which 6 mg/g was constituted by cholesterol present in free form and about 3 mg/g in bound form. In tests 1 and 3 a volatile working fluid constituted by a fatty acid ethyl ester 10 mixture, 6o ethyl ester relative to the fish oil, i.e.
the ratio of (volatile working fluid):(fish oil) about 6:100, was added to the fish oil mixture before subject-ing the mixture to a molecular distillation process. All tests below were carried out at mixture flow rates of 900 15 or 400 kg/h in a molecular distillation unit with an evaporation surface of llmz. Test 1 and 2 were carried out at a temperature of 210°C and at a mixture flow rate of 900 kg/h. Test 3 and 4 were carried out at a lower temperature, 205°C, and at a lower flow rate, 400 kg/h.
20 The amount of cholesterol present in the fish oil mixture in free form was analysed by a method based on standard high performance liquid chromatographic analyses.
Test Temp.(C) Flow rate % added Free cholesterol (kg/h) ethyl es- (mg/g) ter 1 210 900 6 1,4 2 210 900 0 2,4 3 205 400 6 0,2 4 205 400 0 0,4 Table 1: Amounts of cholesterol present in a fish oil in free form after molecular distillation
21 The results in the table above illustrates that it is possible to decrease (to separate) an amount of free cholesterol in a marine oil more effective by adding a volatile working fluid to a marine oil composition and thereafter subjecting the fish oil composition to a stripping processing step according to the invention. It is important to note that the effect by adding a volatile working fluid to a marine oil composition, before sub-jecting at least one stripping processing step, is bet-ter, and more interesting, when the stripping process is carried out at higher mixture flow rates, preferably flow rate in the interval of 80-150 kg/h~mz. Under these condi-tions, the use of a volatile working fluid opens up for a much better utilization of the capacity of the process equipment and a more rapid stripping process.
Another advantage by using a volatile working fluid according to the invention is that the stripping effect is satisfactory at low temperatures [temperatures in the interval of 120 - 220°C] for marine oils. Namely, for ma-rine oils, such as fish oils, and other temperature ac-commodating oils (oils comprising long chains of polyun-saturated fatty acids) it is important to keep the tem-perature load during the processes as low as possible.
But, this is less important for other oils not mentioned above.
Further, the effect of adding a volatile working fluid, compared with no adding of the same, is less no-ticeable in the case when the stripping process is car-ried out at low mixture flow rates [i.e. flow rates < 30 kg/h~m2]. But on the other hand, it is not known commer-cially interesting to carry out a stripping process using low feed rates and relatively high temperatures because the stripping process will take too long to finish. Addi-
22 tionally, today it is a problem for the marine oil indus-try to find effective and rapid techniques that are able to decrease the amount of cholesterol in marine oils at higher flow rates.
The tests above also show that the amount of free cholesterol is reduced from about 6 mg/g to about 1,4 mg/g by adding a volatile working fluid to a fish oil mixture prior to a molecular distillation process, which process being carried out at a temperature of 210°C and at a mixture flow rate of 900 kg/h pr. Here, the amount of cholesterol in free form is decreased with about 75-80 0 .
When the stripping process is carried out at 900 kg/h the amount of free cholesterol is reduced further compared to the stripping process where no ethyl ester (working fluid) has been added, at the same flow rate.
Note that the content of bound cholesterol is less af-fected by the stripping process according to the inven tion. Additionally, the use of very high temperatures, i.e. temperatures above 270°C, isn't of interest. Such temperatures will cause damage to the oil. Too high tem-peratures also can be harmful for the production equip-ment.
Further, the amount (°s) of addition of ethyl ester is also of importance. Addition of at least 4°s ethyl es-ter or an ethyl ester fraction has also generated good results. Preferably, the ratio of (volatile working fluid):(marine oil) is about 1:100 to 15:100 and more preferably, the ratio of (volatile working fluid):(marine oil) is about 3:100 to 8:100.
While the invention has been described in detail and with reference to specific embodiments thereof, it will be apparent for one skilled in the art that various
23 change and modifications can be made therein without de-parting from the spirit and scope thereof.
DEFINITIONS
As used herein the term marine oil also includes ma-rine fat and a fermented or refined product containing at least n-3 polyunsaturated fatty acids, predominately EPA
and DHA from a raw marine oil. Further, the marine oil is preferably oil from at least one of fish, shellfish (crustaceans) and sea mammals, or any combination thereof. Non limiting examples of fish oils are Menhaden oil, Cod Liver oil, Herring oil, Capelin oil, Sardine oil, Anchovy oil and Salmon oil. The fish oils mentioned above may be recovered from fish organs, e.g. cod liver oil, as well as from the meat of the fish, from the whole fish or from fish waste. Additionally, the term "oil and fat" means fatty acids in at least one of the triglyceride and phospholipid forms. Generally, if the start material in the stripping process is a marine oil, the oil may be any of raw or partially treated oil from fish or other marine sources and which contains fatty ac-ids, including polyunsaturated fatty acids, in the form of triglycerides. Typically, each triglyceride molecule in such a marine oil will contain, more or less randomly, different fatty acid ester moieties, be the saturated, monounsaturated or polyunsaturated, or long chain or me-dium chain. Further, examples of vegetable oils or fats are corn oil, palm oil, rapeseed oil, soybean oil, sun-flower oil and olive oil. Additionally, the marine fat or oil may be pre-processed in one or several steps before constituting the start material in the stripping process as described above.
24 As used herein the term edible means edible for hu-mans and/or animals. Additionally, as used herein the term "for use in cosmetics" means an oil or a fat that can be used in products that contributes to enhance hu-mans appearance and/or health, e.g. cosmetic and/or beauty care products. Further, a fat or an oil, being edible or for use in cosmetics, according to the inven-tion can also be a blend of e.g. microbial oils, fish oils, vegetable oils, or any combination thereof.
As used herein the term microbial oils also includes "single cell oils" and blends, or mixtures, containing unmodified microbial oils. Microbial oils and single cell oils are those oils naturally produced by microorganisms during their lifespan.
As used herein the term working fluid is interpreted to include a solvent, a solvent mixture, a composition and a fraction, e.g. a fraction from a distillation proc-ess, that has a suitable volatility, comprising at least one of esters composed of C10-C22 fatty acids and Cl-C4 alcohols, amides composed of C10-C22 fatty acids and C1-C4 amines, C10-C22 free fatty acids, mineral oil, hydro-carbons and bio-diesel.
As used herein the term essentially equally or less volatile is interpreted to include that the volatile working fluids having a suitable volatility in relation to the volatility of the cholesterol present in the ma-rine oil in free form that is to be stripped off from the marine mixture. Further, commonly this is the case when the volatility of the working fluid is the same or lower than the volatility of the cholesterol present in free form. However, the term essentially equally or less vola-tile is also intended to include the case when the vola-tile working fluid is somewhat more volatile than the cholesterol in free form.
Further, as used herein the term stripping is inter preted to include a general method for removing, separat 5 ing, forcing or flashing off gaseous compounds from a liquid stream. In addition, the term "stripping process-ing step" preferable herein is related to a method/process for decreasing the amount of cholesterol in a marine oil or fat by one or more distilling or dis-10 tillation processes, e.g. short path distillations, thin-film distillations (thin-film stripping or thin-film (steam) stripping), falling-film distillations and mo-lecular distillations, and evaporation processes.
As used herein the term "together with", means that 15 the volatile working fluid will be stripped off together with, combined with, or adhering the cholesterol, namely that the cholesterol will accompany the working fluid.
As used herein the term health supplement is inter-preted to include food and food supplement to animals 20 and/or humans, fortification of food, dietary supplement, functional (and medical) food and nutrient supplement.
As used herein the term "treating" means both treat-ment having a curing or alleviating purpose and treatment having a preventive purpose. The treatment can be made
25 either acutely or chronically. In addition, as used herein the term pharmaceutical means pharmaceutical preparations and compositions, functional food (foodstuff having an increased value) and medical food. A pharmaceu-tical preparation according to the present invention may also comprise other substances such as an inert vehicle or a pharmaceutically acceptable adjuvance, carriers, preservatives etc., which all are well-known to those skilled in the art.
26 As used herein the term "oils with a low quality"
preferably means that the oil contains high amounts of free fatty acids, that makes them less useful for nutri-tional purposes and that traditional alkaline refining in such oils is complicated and costly. Additionally, as used herein, the term mineral oil is interpreted to in-clude mineral oil products such as e.g. fractions from distillation processes and white spirit. As used herein hydrocarbons is interpreted to include organic compounds, that are relatively large molecules composed mainly of carbon and hydrogen. They can also include nuclei of ni-trogen, phosphorus, sulphur, and chlorine, among others.
Further, the method according to the invention is also applicable to a variety of sterols including choles-terol. Most of these sterols can, when present on free form, be separated from a marine oil by the described technique as long as the volatile working fluid is essen-tially equally or less volatile than the sterol in free form that is to be separated from the marine oil mixture.

Claims (35)

We Claim:
1. A process for decreasing the concentration of cholesterol in a marine oil in a pharmaceutical composition, the marine oil comprising cholesterol in free form, the process comprising:
(a) adding a volatile working fluid to the marine oil, wherein the volatile working fluid comprises at least one fluid chosen from fatty acid methyl esters, fatty acid ethyl esters, and fatty acid amides, and (b) subjecting the mixture of marine oil and volatile working fluid from step (a) to at least one stripping processing step, wherein an amount of the cholesterol present in the marine oil in free form is separated from the mixture together with the volatile working fluid;
wherein the volatile working fluid is essentially equally or less volatile than the cholesterol in free form that is to be separated from the marine oil mixture;
and further wherein the at least one stripping processing step is carried out at a temperature ranging from 120°C to 270°C.
2. The process according to claim 1, wherein the fatty acid moieties of the fatty acid methyl esters, fatty acid ethyl esters, and fatty acid amides are obtained from a fat or oil obtained from at least one of vegetable, microbial, and animal origins.
3. The process according to claim 2, wherein the animal fat or oil is a marine oil.
4. The process according to claim 1, wherein the volatile working fluid comprises at least one fatty acid ester composed of a C10-C22 fatty acid esterified with a C1-C4 alcohol.
5. The process according to claim 1, wherein the marine oil comprises at least one fatty acid chosen from saturated fatty acids in the form of triglycerides and unsaturated fatty acids in the form of triglycerides, and wherein the marine oil is obtained from fish or sea mammals.
6. The process according to claim 1, wherein the ratio of (volatile working fluid):
(marine oil) ranges from about 1:100 to 15:100.
7. The process according to claim 6, wherein the ratio of (volatile working fluid):
(marine oil) ranges from about 3:100 to 8:100.
8. The process according to claim 1, wherein the at least one stripping processing step is carried out at a temperature ranging from 150°C to 220°C.
9. The process according to claim 1, wherein the at least one stripping processing step is carried out at a pressure below 1 mbar.
10. The process according to claim 1, wherein the at least one stripping processing step is chosen from thin-film evaporation processes, molecular distillations, short-path distillations, and any combinations thereof.
11. The process according to claim 10, wherein the thin-film evaporation process is carried out at a mixture flow rate ranging from 30 kg/h.cndot.m2 to 150 kg/h.cndot.m2.
12. The process according to claim 1, wherein the at least one stripping processing step is carried out at a mixture flow rate ranging from 80 kg/h.cndot.m2 to 150 kg/h.cndot.m2.
13. The process according to claim 1, wherein the volatile working fluid is a distillate fraction from a process in which a mixture comprising at least one of ethyl and methyl esters of fatty acids obtained from marine oil is fractionated by distillation.
14. The process according to claim 1, wherein the marine oil further comprises cholesterol in bound form, and wherein the at least one stripping processing step is followed by:
(c) subjecting the stripped marine oil mixture to at least one trans-esterification reaction with a C1-C6 alcohol under substantially anhydrous conditions, and (d) subjecting the transesterified marine oil from step (c) to at least one distillation process that yields a distillate marine oil fraction and a residue marine oil fraction, wherein the distillate marine oil fraction has concentrations of free and bound cholesterol lower than in the residue fraction.
15. The process according to claim 14, wherein the C1-C6 alcohol is ethanol.
16. A lowered-cholesterol-content marine oil product in a pharmaceutical composition, the marine oil product comprising eicosapentaenoic acid (EPA) and docosahexaenoic acid (DHA) and produced by the process comprising:
(a) adding a volatile working fluid to a marine oil, wherein the volatile working fluid comprises at least one fluid chosen from fatty acid ethyl esters, fatty acid methyl esters, fatty acid amides, and free fatty acids;
(b) subjecting the mixture of marine oil and volatile working fluid from step (a) to at least one stripping processing step, wherein an amount of cholesterol present in the marine oil in free form is separated from the mixture together with the volatile working fluid to provide a lowered-cholesterol content marine oil; and (c) increasing the concentration of at least one of the EPA and DHA in the lowered-cholesterol-content marine oil to a pharmaceutically effective concentration to therapeutically treat hypertriglyceridaemia;
wherein the volatile working fluid is essentially equally or less volatile than the cholesterol in free form that is to be separated from the marine oil mixture;
and further wherein the at least one stripping processing step is carried out at a temperature ranging from 120°C to 270°C.
17. The process according to any one of claims 1-5, wherein the process decreases the concentration of cholesterol in free form in the pharmaceutical composition to 1.4 mg/g to 3 mg/g.
18. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the marine oil comprises at least one fatty acid chosen from saturated fatty acids in the form of triglycerides and unsaturated fatty acids in the form of triglycerides, and wherein the marine oil is obtained from fish, shellfish, sea mammals, or any combination thereof.
19. The lowered-cholesterol-content marine oil product produced by the process according to claim 18, wherein the marine oil comprises fish oil.
20. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil is less than 3 mg/g.
21. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil is less than 1.4 mg/g.
22. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil ranges from 0.2 mg/g to 1.4 mg/g.
23. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil ranges from 1.4 mg/g to 3 mg/g.
24. The lowered-cholesterol-content marine oil product produced by the process according to claim 23, wherein the marine oil comprises fish oil.
25. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the marine oil of step (b) is chosen from raw marine oil and refined marine oil.
26. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein in step b), the volatile working fluid with the cholesterol is derived to a condenser.
27. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the at least one fluid of the volatile working fluid is chosen from methyl esters and ethyl esters.
28. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the volatile working fluid comprises a by-product from a process for producing at least one of methyl ester concentrates and ethyl ester concentrates.
29. The lowered-cholesterol-content marine oil product produced by the process according to claim 16, wherein the at least one stripping processing step of step (b) is followed by:
(b1) subjecting the stripped marine oil to at least one trans-esterification reaction with a C1-C6 alcohol under substantially anhydrous conditions, and wherein increasing the concentration of at least one of EPA and DHA in step (c) comprises subjecting the transesterified marine oil from step b1) to at least one distillation process that yields a distillate marine oil fraction and a residue marine oil fraction, wherein the residue marine oil fraction comprises lower concentrations of both free and bound cholesterol than the distillate fraction.
30. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the marine oil comprises fish oil.
31. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil is less than 3 mg/g.
32. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil is less than 1.4 mg/g.
33. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil ranges from 0.2 mg/g to 1.4 mg/g.
34. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the amount of cholesterol in free form in the lowered-cholesterol-content marine oil ranges from 1.4 mg/g to 3 mg/g.
35. The lowered-cholesterol-content marine oil product produced by the process according to claim 29, wherein the at least one distillation process of step c) comprises molecular distillation.
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